Catalytic polymerization of olefins



Aug. l2, 1952- G- C. BAILEY ET AL CATALYTIC POLYMERIZATION OF' OLEFINS Filed June l5, 3.945

2 SHEETS-SHEET l /Jsmmt oznm soJ Allg- 12, 1952 G. c. BAILEY ET AL 2,606,940

CATALYTIC FOLYIIIERIZATION oF OLEFINS Filed June 15,1945 2 SHEETS-SHEET 2 CARRIER OF sILICA GELOR .SDIUM OF sILICA GEL ACTIVATED SILICATE ACID wITH OI-Io PER CENTOF ALUMINA IMPRECNATION wITH AQuEOus fgTTV/LH sOLuTION OF NICKEL NITRATE OF SIMCA HYDROGEL I DRYING WASHING I HEATING TO DRIvEOFF ALL COMBINED NITROGEN OxIDEs AND CONVERT NICKEL NITRATE WET S'L'CA CE'- TO NICKEL OxIDE IMPRECNATION ACTIVATION 0F NICKEL OxIDE W'TH AQUEOUS BY HEATING TO 4oo7ooC y SOUT'ONST FOR ONE HOUR IN STREAM "I" 'I OF OxIDIzINC CAs WASHING FINIsI-IED CATALYsT READY FOR usE IN OLEFIN POLYMERIZATION DRYING CONTACT wITH OLEFIN AL'PHAT'C OLEFIN TO EFFECT C2' C4OLEF'N PoLYMERIzATION POLYMER FEED A PRODUCT THEREOF A lNvENToRs GCALEY `I.A.RI:IO

Patented Aug. 12, 1952 CATALYTIC POLYMERIZATION OF OLEFIN S Grant c. Bailey and James A. Reid, Barnesville@ Y Okla., assignors to Phillips Petroleum1Com-`V pany, a corporation of Delaware Application June 15, 1945, Serial No. 599,530` l( l y This invention relates to the catalytic polymerization of olens especially the low-boiling normally gaseous olens, namely, ethylene, propylene, and the several butylenes, viz. butene-l, butene-2 and isobutylene, to produce higherboiling higher molecular Weight olenpolymers. The invention also relates to an improved catalyst 'particularly adapted to use in such polymerization, and to a method of making such a catalyst.

This application is a continuation-in-part of our copending application, Serial No. 435,888, led March 23, 1942, now U. S. Patent 2,381,198 granted August 7, 1945.

The conversion of olens to hydrocarbons of higher molecular weight by polymerization reactions is well known. In some instances, such polymerizations may be accomplished solely by the application of heat and pressure, but in many cases the use of a catalyst is desirable. In general, catalysts cause polymerizations to proceed at lower temperatures, decrease-the number and types of polymeric materials formed, and increase the vyield of desired products. Many individual catalysts already have been found that are active for the polymerization of olens. These include active earths, such as oridin; acids, such as sulfuric, phosphoric, and hydrouoric; the active metal halides, such as aluminum chloride, boron fluoride, zirconium Vtetrachloridaand the like; and also other materials, among which are phosphoric anhydride and silica-alumina gel. It has been established that no catalyst is the exact equivalent of any other catalyst and thatproducts diiering not only in molecular weight, but also in molecular structure may be prepared through the use of dierent catalysts, when polymerizing the same olens.

We have now found a new and useful catalytic system for the polymerization of olens to higher molecular weight hydrocarbons.v

An object of this invention is to provide a catalytic polymerization system for the conversion of olefns to products within a desired molecular weight range.

Another object of this invention is to provide a catalytic system for the conversion of olens to polymers which possess desired physical and chemical properties.

Another object of this invention is to convert olens to polymers possessing limited branched chain structures.

4- Claims. (Cl. 26o-683.15)

Another object of this invention is to polyj 2,.; A VAnother object-ris.; to, provide faf new andimproved catalyst which is'especially useful jin polymerization of olens to higher molecular weight hydrocarbons. l 1 i Anotherobject is to provide animproyedmeth'- od of making `such a catalyst. {f1-Tin" Many vother objects and advantages 'of-,our

invention will become apparent-to those skilled in the art from the following'description. Y

In the accompanying"drawingjFg. l1 shows diagrammatically by means 'of a flow s heetan arrangement of apparatusr suitable, for the practice of our. invention. Fig. 2 portrays ja flow diagram Villustrating a preferred Vmethod of preparing the catalyst'inaccordanceiwith the present invention. v A

GENERAL if? We have now found that olens can be polyy merized to simple olefin hydrocarbon polymers in a markedly improved manner by means of `a catalystcomprisng nickel oxide Supported on silica gel as a carrier. The nickel oxide employed as the'sole effective catalytic element in accordance with the present invention is preferably in an active form as a result of activation in a manner described in detail hereinafter, typically by heating to a temperature of from 400 to '700 C. and' preferably in an atmosphere or stream of an oxygen-containing gas for a suitable period of time, usually one hour.

We have found that the nickel oxide catalyst of our parent application Ser. No. 435,888, above identified may be greatly improved by the use of silica gel as a support. We have further found that alumina,V typically used in small amounts, preferably from 1 to l0 percent by weight vof the silica gel carrier, is a true promoter for such a catalyst.

As used herein the V`term nickel oxide denotes any oxide of nickel, or mixture of oxides of nickel but has particular reference to the form of oxide of nickel which results from activation by heating in an oxygen-containing atmosphere such as air in the manner more fully described below. The chemistry of the oxides of nickel appears to be `not fullyv understood. The existence of nickelous oxide (NiO) and nickel dioxide (NiOz) appears to be established beyond doubt. Inaddition to these oxides, nickel sesquioxide (NizOa). nickelosic oxidev (NisOt) and nickel peroxide (NiOt) have .been reported. While we are not limited to any theory it may be stated that the activation step of our invention converts the nickel to an oxide ormixture of oxides. Whether any such oxide is a single oxide or a mixture of acoaefio heated strongly in oxygen, give the oxide NiiOi.`

Mellor and Parkes state that Ni203 is formed as a black powder when NiO is heated in air and when the nitrate or carbonate is ignited in air at a low temperature but is thought to be actually a mixture of NiOz and NiO. While the cornposition of the nickel oxide used in accordance with the present invention is not now known to us with any certainty, we do describe herein a method whereby it mayV be reproduced or duplicated with absolute certaintyv by thoseI skilled in the art.

The catalyst may be prepared by aV wide Vvariety of" chemical routes, the essential feature of the invention being the use of silica gel, either alone or preferably with asmall amount of alumina` as acatalystpromoter, as a carrier or support for the nickel oxide catalyst of our parent application above-identified.y An important additional feature of the invention is activation of the nickel-oxide as a nal step'in the preparation of thecatalyst, this activation involving heating at atemperature inthe range of 300 to '700 C. and preferably-400 to 60Q C. for a length of time of from one-half to 12 hours, commonly one hour.

Y PREPARATION Oli"` CATALYST Catalysts useful in theip'r'ese'nt invention may be prepared by Yimpregnating silica gel with a nickelcompound which is readily decomposable to nickel oxide upon heatingV to moderately Vlelevated temperature followedv fby heating to` effect such conversion to the oxide and then heating in an oxygen-containing atmosphere or stream to effect activation of the resultingx nickel' oxide. The nickel compound employed for the "impregnation and as a Source of nickel oxide may be nickel carbonate or basic nickel carbonate preclpitated within the interstices of the silica gel in known manner and' then heated to drive off carbon dioxide and any'water.' Under some circumstances the precipitated carbonate may be reduced to metallic nickel by heating to a temperature in the range of 300 to 400' C. in a stream of hydrogen. This reduced nickel AWhic'ri/,is a highly pyrophoric active hydrogenation catalyst, can be converted to a polymerization catalyst by heating it' to a temperature in the range of 400 to 700 C. and at least partially oxidizing it, as in astream of oxygen diluted with an inert gas such as nitrogen. This oxidation step is highly exothermic, and without suitable precautions the actual temperatures in the interior ofthe catalyst mass may greatly exceed the temperatures indicated externally; thus under such conditions active catalysts have been` prepared by heating in a furnace in which the indicated temperature was as low as 300 C. or evenlow'er, although'we believe that actual temperatures within the mass were appreciably higher.V The best results are obtained, however, by keepingV the catalyst at a uniform, controlled temperature during this oxidation step. This can be accomplished by agitating the catalyst and using an oxygen-nitroi gen mixture containing from about one to ten per cent oxygen. Under these conditions local overheating is prevented, and uniform oxidation is obtained. The extent of oxidation under these conditions is not critical. Activ-e polymerization catalysts have been prepared using as little as ten per cent and as much as 50G per cent of the amountof oxygen theoretically necessary to ccmbine with the metallic nickel initially present to 4form Nif), although the activity apparently passes through av maximum when treated with about 100 to 153 per cent of oxygen theoretically required to form this oxide.

The reduction and oxidation steps just described are'not always essential in the preparation of active polymerization catalysts from nickel carbonate on silica gel. The carbonate may be decomposed to nickel oxide by heating in a stream of air, or in a dilute mixture of oxygen in an inert gas such as nitrogen,.or in a stream of an inert gas lsuch. as nitrogen, or in vacuo. In all such cases the' resultant nickel oxide is catalytically active if the decomposition has been carried out at. a :temperature in the range of about Lth 700 C., or if the nickel oxide is heated to a temperature in this rangev after the decomposition has Vbeen completed ata lower temperature. Catalysts Vthat havebeen treated with oXygen in this activating temperature range have somewhat higher activity, and longer life than those prepared. in the absenceloi oxygen. We prefer to use nickel nitrate asthe source of nickel in practicing our invention. For example, the granular' silica 'gel carrier may befimpregnated with an aqueous solution of nickel nitrate, whereupon the nitrate is decomposed to the oxide by heating under conditions such thatV substantially all combined nitrogen oxides vare removed, followed'byactivation of the resulting nickel oxide preferably by heatingin'angoxygen-containing. atmosphere at. a' temperature of` -froni30() to '100.o C. and' preferably LlOO'to GOOFC. before the decomposition and.v activation', may be carried out in ay vsingle'h'eatingstep.Y For' example, the impregnatedcarrier: may be heatedin a. current of air. at5'0" C; for: approximately' one hour whereby the-activation ofthe nickel 'oxide :proceedsv as fastias it is formed by the decomposition reaction, the. streanr ofi airV ser-ving both to carry olf the nitrogen oxides as they `are liberated and to supply oxygen for the activation of' the nickel oxide..

While the heating of thesilica gel vcarrier impregnated with the aqueous nickelV Vsalt solution such as the nitrate to convert the salt to nickel oxide is preferably done ina stream ofanoxygencontainingy gas, it may, though 'less' preferably, be

lcarried out in an oxygen-free. gaseous stream such as nitrogen or in a vacuum,` vthe important. consideration being that the :nitrogen oxides 'are rapidly removed andA that no reaction Witha. reducing gas takesplace. i

Th-e silica gel may be-inzdryrgranular. formV or Wet with water, prior to impregnationxwith. the decomposable nickel compound; In: certain. circumstancesjit maybe found preferable to-employ hydrous silica gel which has nommen-'completely dried in the processY of itsl manufacture. Thus hydrous silica gel istpreparedby mixinga watersoluble silicate, usually sodium; orf potassium silicate with a mineral acid to effect formation of a'silica hydrogel whichiswater-washed to remove soluble ions. The resulting hydrogel, either without anyvdrying or with'` only 'partial` drying, is impregnated `with the nickel-compoundas deon silica gel.

-iaeoaefio l'scribed above. --s explained below. a decomposable aluminum salt may be employed inconjunction with the decomposable nickel salt .in

PERCENTAGE OF NICKEL OXIDE The percentage of nickel oxide in the'k finished catalyst may vary widely. Ordinarily, it ranges Vupwardly from one-tenth (0.1) of a per 'centby weight of nickel on a reduced basis, i. e. ,jexpre`ssed jas elemental nickel, based on the` Weight ofjthe silica gel, upwardly to any practical upperylimit.Y

Usually the upper limitof nickel oxide is' that above which the valuable properties of the 'silica gel carrier or the carrier ofsilica gel activated with alumina would be obscured. Generally the concentration of nickel oxide will not exceed 35 per cent of elemental nickel by Weig-htA based on the weight of the silica gel. More commonly the nickel oxide content will range from 0.1 to weight Yper cent of elemental nickel based on the silica g-el. Such levels `oi nickel oxide give a'highly active catalyst'and since the resulting catalyst is much less expensive than when higher percentages of nickel are employed, we prefer to use the 0.1 to 5 per cent range.

USE OF ALUMINA AS PROMOTER An important and preferred feature of .the present invention resides in the use of alumina in small amounts in the catalyst composition. As is illustrated in the examples given below, we have found that alumina is a true promoter for a catalyst comprising our nickel oxide supported The amount of alumina employed may vary widely. Ordinarily We'prefer to employ alumina in an amount ranging from 1 to 10 Weight per cent of the silica gel. Amounts -smaller than one per cent may be used |but the promoting effect may not be substantial. ySimilarly amounts of alumina above per centvmay be employed but the additional promoting eie'ct may not justify the additional cost. In any event the amount of the alumina should never exceed 50 per cent of the weight of the silica gel. The effect of the alumina promoter is most pronounced at the 1 to 10 per cent level.

The promoter may be incorporated into the catalyst in a. wide variety of manners. It may be added to the catalyst as such but this-is often an unsatisfactory method. We prefer to impregnate the silica gel with an aqueous solution of an aluminum salt which is decomposable upon heating to alumina, almost invariably aluminum sulfate or nitrate, and to then dry and heat to convert to alumina in a highly active form'which is capable of exerting maximum promoting effect on the catalyst. This impregnation with the aluminum salt solution is preferably performed upon the silica gel while it is still Wet with water in the process of its manufacture. The resulting silica gel activated with alumina is then impregnated with an aqueous solution, nickel nitrate, which is subsequently converted to the oxide and Y activated in the manner described in detail above.

Silica gel activated with alumina by impregnaf tion of Wet or partially dried silica gel with an l aqueous solution of an aluminum salt convertible alui'nina gel, gels made by precipitation of alumina gel onto.` silica gel, and gelsmade by'mX- ing the separately formed gels. +15

We often `prefer to use commercially .silica gel activated with alumina as our,` carrier.

For instance we mayfuse the material knownin the trade as ,Phillips silica-alumina catalyst which is made by activating'silica gel Withfalumina by impregnating Wetnewly-prepared silica gel with a .solution of; an aluminumA salt to .effect activaton'of the silica gel, washing thelactivated gel, and drying, as disclosed in JU. S. patentsyto AMcKinney 2,142,324 and 2,147,985,l Hendrxtiafl- 2,342,196,. ari-dto Hachmuth 2,349,904..L See also 1U." S. patents to' Connolly 2,257,157, and Cross part of the aluminum, presumably in the formof a hydrous oxide or loose hydroxide rcompound formed by hydrolysis, selectively adsorbed by the hydrous silica, and is not removed by subsequent washing.` This selective adsorption is attested by a decrease in the aluminum content yof the activating solution as well kas a decrease in pH thereof as activation progresses. The resultingcarrier will contain a major portionof -silica and minor proportion of alumina. This minor portion of alumina will generally not be ingexcess of 10 %by weight and will more often'and generally more preferably be between 0:1 and 1.5,or,2,% by weight. In this procedure ,the water-soluble silicates such as sodium silicate and thecommercially available mineral acldsaregemployed, sulfuric and hydrochloric acids-are preferred on economic grounds althoughany Aacid may be used which will provide suitable hydrogen ionY concentration and precipitate a silica hydrogelgof proper consistency. Thus, phosphoric, acetic .and nitric acids may be used. The gel formed should be acidic and should be washed freel ofl excess acid. prior to activation. It may be partially dried prior to activation but the extent of drying-is carefully controlled since the eventual activity of the activated silica gel is apparently dependent on the maintenance of the.. hydrous oxide composition prior to the activation with alumina. Any water-soluble hydrolyzable salt of alumina may be used in preparing the salt solution'ffor activation, the sulfate or chloride beingv preferred. Alternate salts include aluminum acetate or nitrate. The adsorption of the hyd-rous aluminum oxide proceeds smoothly with hydrated silica gel, Whereas with dried silica the adsorptionand the activation are often much less satisfactory. The resulting active silica gel is rinsed free ofthe salt solution and a moderate concentration' effector curing may be obtained by partial drying of the rinsed gel. The final washing then serves to remove unadsorbed salts and free acid, and the nal drying which is performed at moderate temperatures produces hard, brittle granules'of gel containing negligible Vvquantities of compounds other than silica and alumina.

The resulting gel-type silica-alumina material consists essentially of silica and alumina f with 7 variant quantities of water. 4'Either salts or oxides are preferably absent from the carrier. VThe alu- V-minamay be present in .minor activating Vquantities of from 1 to 10 weight per cent of the silica.

-In many cases, .the activity may be as great with 1 to 5 per cent of alumina as with .10 to 15 .per cent. .Still greater amounts of alumina up to 50 -weight per cent may be incorporated .if desired,

althoughthe physical characteristics and activity of .the .carrier may :be adversely affected. The

Vworkof Elkinfetal. reported in Ind. and Eng.

wet with an aqueous solution of the aluminumy lsalt and a compatible and appropriate nickel salt, whereupon the impregnated silica gel is driedand heated to remove water and convert'the aluminum salt `to alumina and the nickel salt to nickel oxide, followed by' activation of the nickel oxide as described above. Use of aluminum nitrate and -nickel nitrate in this embodiment of our invention is very advantageous.

Another. preferred method of incorporating alumina promoter into the catalyst i-s to impresnate the silica gel Ycarrier with an aqueous solution of an aluminum salt decomposable to the oxide simultaneously with the impregnation with an aqueous solution of the nickel salt. In such event 'the aluminum 'salt should be compatible with the nickel salt and notinterfere with the subsequent decomposition and activation steps applied thereto. Ordinarily, the aluminum salt will have the same negative radical as the nickel salt. An unusually advantageous method of realizing this type of incorporation is to. impregnate the silica gel with an aqueous solution vof nickel nitrate and of aluminum nitrate, dry,` heat to decompose the two salts to the corresponding oxides with removal of all combined nitrogen oxides in .the manner described above for nickel nitrate, and then activate the nickel oxide in the mannerY set forth above.

vIf desired the nickel salt such as the-nickel .nitrate or the mixture oi nickel and aluminum salts impregnated onto the silica ge'l carrier may `be decomposed in `a stream of an inert gas such as nitrogen at a temperature in the range of 350 to 375 C. followed by heating the nickel oxide thus produced to a temperature in the range of 400 to 700 C. in Aa stream of diluted oxygen/such as au'. Y

Other salts of nickel or of nickel andalurninum which decompose to nickel or nickel oxide or to nickel and aluminum oxide on heating to temperatures in the range of about 100 to 500 C. may likewise be used in the preparation of catalysts of .the present invention. The use of nickel sulfate may not be desirable because oi the. diiculty of vgetting rid of all, oi the combined sulfuroxide.

Nickel nitrate is preferred.

` POLYMERIZATION Temperatures in the neighborhood of 100 C. mayv be superior since at'such levels polymerization is accelerated without undue side reactions. Above a polymerization temperature of about 200 C. hydrocarbonsvother than olen polymers begin to be formed.

If the polymerization of the present invention be carried out at temperatures above about C., say from 160 C. upwardly to say 200 C.. and in the presence of hydrogen, hydrogenation will take place.. We ordinarily operate at ternperatures notover150 C. and in the absence of hydrogen or other reducing agent.

While any aliphatic 'low-boiling olen'having from two to four carbon atoms. per molecule may be polymerized by the p-resent invention, 'we iind our invention to be 'especially advantageous when applied to ethylene'which is extremely diicult to polymerize smoothly and satisfactorily by methods heretofore proposed.

High pressures favor the polymerization reaction, but under suitable conditions the reactions may be carried out under a very wide range of pressures, from as low as atmospheric or below, to as high as 2,000 p. s. i. or above. High pressures not only increase the rate of polymerization,

but also increase the average molecular weight of the polymer formed.

The polymerizations using our catalyst may be carried out in either liquid or gas phase. In gas phase polymerization, the reaction must be carried out under conditions whereby the exothermic heat of reaction does not cause excessive local overheating of the catalyst, or a general rise in temperature above the desired operating-range.

This can be accomplished by suitable design of a catalyst chamber to allow good heat transfer, and by controlling the rate of introduction of charge stock. In many cases liquid phase operation is preferred, and pressures such as to insure substantial or complete liquid phase operation are advantageous. Liquid phase operation facilitates control of reaction temperature and contributes to catalyst life by diminishing the deposition of high molecular Weight, or other nonvolatile or insoluble, materials on the catalyst surface. When polymerizing an olefin or olenic material above its critical temperature, itis often desirable to'insure that a liquid phase is present by carrying out the Vreaction in the presence of an inert higher boiling materiaL especially a higher boiling normal paraffin or cycloparafn. A diluent, either higher or lower boiling than the charge, may also be advantageously used in other cases in which the polymerization temperature is not above the critical temperature of the olefin or olefin mixture being polymerizati.

The polymerization catalysts vof our invention Yare readily `deactivated or poisoned by various Aadapted to the particular case, such as fractionation, extraction with adsorbents or solvents, chemical treatment, `and `the like. We have found, however, that `for best "results from our catalyst, vextreme 'puriiication of `the charge is desirable, in orderto remove 'the smallest traces VVof poisonousmaterialsr For example, an oleiinic charge, containing less than 0.5 per cent of nona trace of sulfur compounds, could not be vpolymerized in our system, whereas by passingfthis charge through a bed of nickel on silicaA gel hydrogenation catalyst at `200 C., and through a sodium hydroxide on asbestos adsorbent at room temperature, more satisfactory polymerization was obtained. We have also found that the charge to our polymerization catalyst can be puried by contacting it with a metal which forms alkyl derivatives reactive with water, such as sodium, commingled with a metal selected from the iron group which is active as a catalyst for hydrogenation reactions, such as nickel, at a temperature between 50 and 150 C. Such a purification process is more specifically disclosed in our copending application Serial No. 430,834, led February 13, 1942, now U. S. Patent 2,378,969 granted June 26, 1945. c

We have found the activity of our polymerization catalyst is increased by polymerizing in the presence of an alkali or alkaline earth metal. The metals may be nely divided, but are p-referably in liquid state to obtain the most intimate contact between metal and reactants. In order to obtain liquid metals at the operating temperature, alloys-or amalgams of the alkali or alkaline earth metals may be used. When using the catalyst in the presence of a metal such as sodium or potassium, the maximum temperature of operation is limited by the reaction of the olen and the metal. For example, ethylene readily reacts with sodium at temperatures above about 200 C. producing an inactive constituent in the system. The exact mechanism by which these added metals increase the polymerization activity is not known, but it may be that they act as superpuriication agents and remove from the catalytic system traces of materialsthat are not removed in the pre-treatment of the charge.

It is desirable to establish intimate contact between the reactants and the catalytic materials, in orderA to obtain the most rapid reaction. Vigorous agitation has been found al satisfactory means of establishing the vnecessary contact, although other means, such as rapid flow of the reactants through the catalyst mixture may also be employed. The time of contact between olenic reactants and our catalyst to produce polymerization may vary over a, wide range. We have found that a contact time as low as 30 secondsat atmospheric pressure and in the preferred temperature range is sufficient to polymerize most olens to an appreciable extent. However, higher extents of conversion arepossible when a, longer contact time and/ or higher pressures are utilized under similar temperature conditions. Contact I times of'3 and even 12r hours are not uncommon when polymerizing olens in the presence of our catalyst.' Y Y l f Polymers are formed when `operatingwithin the temperature range previously discussed, but the temperature for optimum yield depends `to some extent `upon the olen charged and the catalyst used; however, it can readily be determinedl by trial for any specific charge stock.'

and/or any specific catalyst preparation.

A wide variety of `olei'inic compounds may be converted to polymers in our catalytic systems. The oleins which are converted to polymers most satisfactorily are the low-boiling olefins, such as ethylene, propylene, butenes, and the like.

The product obtained, and the extent of conversion, may vary considerably with lthe olefin used as charge stock. For example, in a system containing nickel oxide catalyst together withA similar conditions was found to comprise mainly mono-olei'ins containing 6, 9, and 12 carbon atoms per molecule. Isobutylene was converted'at a relatively moderate rate at a temperature of 30 C. to polymers ranging from vdimers to viscousoils. Other oleins, such as butene-2, pentene-l, and the like, were also found tol be polymerized by our catalyst.

The olenic polymers obtained by the conversion of oleiins using `our nickel oxide catalyst appear to result from simple, straightforward polymerization, and may range from dimers to high molecular weight solid hydrocarbons. These Vproducts usually contain no tertiary-base olefins, or at most only a minor proportion, unless the olefinic charge contains tertiary-base olens.

quently undergo isomerization, cyclization andother secondary changes.

In some cases the total polymer may be used as produced, but it is generally desirable toseparate it into various fractions, for use in spe- V ciiic applications. Some of these fractions may be used as raw materials for the synthesis of valuable organic compounds, or they may be further polymerized using catalysts such as aluminum chloride, to produce polymers in the viscosity range of lubricating oils, or fractions of the product may be hydrogenated and used asy a fuel for internal combustion engines, or used in any other application wherein mono-olefins or their derivatives are desired. I

The operation of a particular modification of our invention willnow be described in connection with Fig. 1 of theaccompanying drawings.

An olefin-containing charge stock from any suitable source, not shown, is charged through pipe I 0 controlled by valve II to a purifier I2 wherein any undesired reactive constituents deleterious to o ur polymerization catalyst such as those previously discussed, are removed. The

purified olenic material is passed from purifier I2 through pipe I3 controlled by a valve I4 to av polymerization zone I5. The polymerization zone I5 will comprise one o r more' catalytic polymerization chambers with associated heating or cooling and temperature controlmeans as may be found necessary in any particular application of. our invention. These polymerization chambers n may be batch-type chambers in which oleiinic material is vigorously stirred withv a mixture of a catalyst, chambers in which aY stationary body of catalyst is employed and in which the olenic material is polymerized, continuously, or the like.'v 'When the initial charge stock does not contain There is also a minimum. of chain branching, as is indicated b y the waxy nature' 1l undesirable reactive material, the puriiier I2 need. notV be used, in. whichA case the charge is. passeddirectly from pipe Iii through pipe I6 controlled. by avalve Il to polymerization zone I5, valves. I.I and I4 being closed.

The polymerized. material passes from polymerization zone I5 through a pipe I8 controlled by valve. I3 to separating means 2d which will comprise cooling and heating devices, fractionatingA columns, filtering equipment, and the-like suitable for the particular type of operation employed When a flowing catalyst is used in the form of a slurry, or the like, all or a part of the catalyst may be present in the material passing through pipe. IS- and the removal of such material-as Well as fractionation of. the products is included.- within the separations carried out in separating means 2G.. Spent catalysts and/or catalysts suitable for recycle to the polymerizationzone-may be removed through pipe 2.I oontrolledby a valve 22.*for reviviiication and/or regeneration as may be necessary. Unreacted olens and-olefinpolymers lower boiling than those desired in the product may be separated and returned to the polymerization zone through' a pipe. 23.l controlled by valve 2li. Any undesired low-boiling material such as low-boiling paraffins,. which may accompany or be added to the olens charged to the polymerization zone, may beremovecl through pipe 25 controlled by a valve 26. Other hydrocarbon material, and/ or any tar or sludge-like material, may be discharged from the systemthrough a pipe 21 controlled by a Valve 28.A One or more polymer fractions having. a desired boiling range. or other desired characteristics may be. recovered. fromV the-system as products in suitable. streams represented by the material passing through pipe- 30 controlled by a- Valve Si and. through pipe 32 controlled by valve 33.

As will be. shown more specifically by examples presented hereinafter, the polymers produced by the practice. of.V our inventionrange from dimers and; trimers to polymers. having molecular weights within. and above those corresponding to hydrocarbons inthe lubricating oilv range. The low-boiling polymers. may be used as such, as special solvents or as raw materials for subsequent chemical conversion operations. It isa feature of. our invention that, especially with certain low-boiling oleiins, the polymer products are essentially straight chain, aliphatic hydrocarbons with a negligible. amount of branching, and in such.- cases the-loW-boiling polymers are not suitable for use as. high octane number fuel stocks, although in some. instances in which loi-v octane product is desirable orV suitable, the polymers may be so.- used. Some or' the higher boiling. polymers in the lubricating oil range are Wax-like and may be used as substitutes for naturally occurring. viaxes, especially after a complete. saturation as by non-destructive hydrogenation. Because of their characteristics o being solid. under ordinary conditions such waxlike polymers are not suitable for use. directly as lubricatingoi-ls, but4 may be readily converted` into. lubricating. oils or stocks by any one of a number of. processes which may include partial depolymerization with polymerization ci the olens. so formed in the presence of another catalyst such as zirconium tetrachloride, alkylation of an isoparaiiin or ci an aromatic hydrocarbon, alkylationor polymerization in a metal halide-catalyzedsystem. and the like. which are lower boiling. than such Wax-like products may also be. converted into lubricating oilsY Polymers l as. by polymerization with asuitablemetal halide catalyst, alkylation ofV other. hydrocarbonmaterials, or the like.

Whenfit is desired to convert such. a polymer product. to a. lubricating oilV stock, this may be accomplished by passing the. selected polymer fraction iroma pipe 3i] through a pipe 35. controlled by avalve 36 to a second reactionv zone 3.1. wherein a. further chemical conversion, such. as herein discussed, takes place. When it is desired t0 alkylate polymer product rwith another hydrocarbonmaterial, such. as an aromatic. hydrocarbon from an outside source, such ahydrocarbon material may be passed to reaction zoneY 3lthrough apipe 38 controlled by .avalve 39. When ajcatalyst is used in zone. 3l. it may be charged thereto in admixture with the material chargedv through pipeV 38 or through other means not shown in the drawing. The eiiluent of reaction-` zone 3l is passed through a pipe-49 controlled by a. valve llI to asuitable separating means illustrated byV ractionating column 42 wherein any desired. separationY of this eiiluent into a lubricating oil stock and one or more other-fractions may be obtained. Adesired lubricating oil stock is recovered as a product of the combined process through a pipe- Flaconi-.rolled by a valve 44, and other.. fractions separated from the eiiluent ofthe reaction zone are recovered through one or more outlets represented by a pipe 45 controlled bya valve 46.

Itis. to be appreciated that the now diagram of Fig. 1 is diagrammatic only; the various pieces of equipment illustrated andv discussed are conventional in nature, and in. any application. of our invention there Will be associated with the individual units shown: various pumps, heaters, coolers, reflux. accumulatore,Y heat exchangers, fractionating columns, temperature indicating and control devices, and the-like, known in the artand Which may bev suitably supplied for. any particular case by one skilled in the art following the. teachings of thereaction conditions and material ilowsdisclosedv and discussed hereinf Figure` 2 of. the. drawings-isA self-explanatory. Following are a-series einen-limiting examples Whichillustrate the present invention. VExamples 1 and2 show the superiority of a catalyst prepared using silica gelas the support in accordance. with the present invention over a catalyst supported on kieselguhr as'was disclosed. in our application, Ser. No. 435,888 (now U.. S. Patent.

. Example 1 Acatalyst of nickel oxide supported on kieselguhr'was prepared as follows: Nickel carbonate was-precipitated upon kieselguhr byslowly adding sodium carbonate solution to a Well stirred suspension of the kieselguhr in an aqueous solution of nickel nitrate. After ltering, Washing,v and drying, the nickel carbonate-kieselguhr mixture Was formed into small pellets. carbonate Was then decomposed, and the catalyst simultaneously activated', by heatingy in a currentv The nickel y lecte'din 235 minutes. J'The4 irateiioffpolymer formation was 25 mLper hour l"per-100 g.' ofcata-l lyst.

jgEwfble'Zf Y The catalyst' for this lexample. was prepared in the following manner.,G'ranular lsilica,gel was soaked in an aqueous ,solution contair'iingl/zlpen cent'by weight of nickelA nitrate '.,hfexa'hydrate- The silica gel rWas'.tallrenvfr'om the solutionandrv d ried in air. This material oonta'ine'dOA percent nickel on a reduced basis. A` The 'nickel nitratewas.

decomposed, and the` catalyst simultaneously ac.-

tivated, by heatingA in a current of air'at 590 ,C. for 1%; hours. The iinishedv catalystecontained over the catalyst described in Example 1 is readily seen. The following examples show that alumina: is a true promoter for a catalyst.comprisingnickel oxide supported on silica gel.

' Example-3 VA polymerization catalyst was preparadas,fol-,-` lows. Highly active silica-.alumina gel of-thet'ype known as Phillips silicaalumina` and contain-Q ing approximately 1.5 weight per cent of alumina was prepared in the manner described above by soaking wet silica gel in a solution of an aluminum salt, washing, drying, and screening the resultant product to uniform size. Upon activating by heating to a temperature of about 300 C., lthis catalyst is very active for the polymerization of some olens, such as isobutylene. For this experiment a portion of the catalyst was heated in a stream of air at 500 C. for 1 hour. Commercial ethylene was passed over the catalyst at a pressure of 200 p. s. i. and at room temperature. The eliuent gas was passed through a trap held at a temperature of -75 C. No liquid polymer was collected in one hour.

Upon raising the temperature to 300 C. a small amount of polymer was formed.

This example showed that silica-alumina gel catalyst is substantially inactive for the polymerization of ethylene.

Example 4 A catalyst was prepared which consisted of 83.3 per cent alumina and 16.7 per cent nickel on a reduced basis. In 8575 ml. of distilled water were dissolved 1272 g. of Al(NO3)3-9I-I2O and 91.83 g. of Ni(NOa)26H2O. Excess NazCOs was added to precipitate all of the nickel and aluminum as the hydrated oxides. The precipitate was filtered, washed, them air dried. A portion of this material was heated in a current of air at 600 C. for one hour. The sample was transferred to a high pressure autoclave, heated to 110 C., and ethylene was slowly admitted until a total pressure of 485 p. s. i. was reached. No reduction in pressure occurred over a period of several hours, signifying that the ethylene was not being polymerized.

In comparison to this, under similar conditions, active catalysts polymerize ethylene at a rate which results in a pressure drop of 8 or. '9 pou'nds per minute using acomparable weight ofc talyst.

The two parts o f this example demonstrate thepromoting `eifect of alumina upon ascatalyst comprising nickel oxide on'silica gel.

VA -catalystwas prepared linthe following man-V Granular dry silica gel was soaked in av ner. solution consisting of 2,0'per cent by weight nickel nitrate hexahydrate. The gel wastakenffromf the solution, excessliquid allowedvto drain pff,` and thematerialwasdried in air. The catalyst was activated by heating in a. streamof'air at. This material contained.

500. C. for one hour. 3.1 per cent nickel.. Y

For comparison with the abovecatalyst asamg; ple of the same silica gel wassoaked in aqueous solutioncontaining 2 0per centby weight nickel nitrate hexahydrate and 12%4 per cent by weight aluminum nitrate enneahydrate. The gel was removed from the solution, dried, and activated by heating at 500 C. for one hour. Theiin---A ished catalyst contained 2.6- per cent nickel. The

exactalumina content of theresulting cat e a)lyst4 is not known since -it Awas not specifically anal-.f lyzed nor can it be lcalculated with high'accu-- racy. However, the catalyst can be conveniently' reproduced since its preparation is suiciently ability to polymerize ethylene at ".v C.,` The initial activity'of the catalyst containing.the a1u minaV was v3.1 times .the activityofthecatalyst I that did not'contain alumina.

This example, along with Examples Sand 4, shows that alumina is a true promoter for this,

typeof catalyst.`

As was pointed out in application, Ser. No. 435,888 (Patent 2,381,198),`an important'step in the preparation of our catalyst is the activation by heating at an elevated temperature. This is further illustrated by the following experiment.

Example 6 The catalyst for this example was prepared by treating a silica-alumina gel carrier with a solution of nickel nitrate. carrier was that known as Phillips silica-alumina and was made as described in detail above and in Example 3. It contained approximately 1.5 weight per cent of alumina. The finished catalyst contained 1.5 per cent nickel. Samples of this catalyst were activated for one hour at .diierent temperatures and their activity for the polymerization of ethylene was tested. The results are presented in the following table.

lrtef Relative Activity soo 4.3

The silica-alumina gel accolse@ '115A process" for' polymerizing. a; normally gaseous olefin hydrocarbon to form higher molecular Weight olefin hydrocarbons which comprises contacting suchY an olen hydrocarbonv under polymerization. conditions including a temperature in the range-of' 0-D to 150 C. With-a poly-1 merization catalystv consisting essentially of a minor proportion of nickel oxide dispersed on a major proportion of silica gelcontaining an amount ofy alumina asapromoter in the range of-f1 to 1-0 Weight per cent based on theWeigh-t of-thesilica gel, the-nickel-in said nickel oxidek ranging-from 0-.1 to 5 Weight per cent of: the

silica gel, saidcatalyst having'heen activated by'- heating in an oxidizing atmosphere ata temp'erature-in'the-range of 400 to 700 C. fora time inrit-he rangeof 0.5 to 12 hours-r and recovering a polfymerizedV higher-- molecularV weight aliphatic ol'en hydrocarbon from the process.

' y2'; A` process for polymerizing a normally gaseous' olefin hydrocarbon to form higher molecular'weight olen hydrocarbons which ct'imprises contacting such an olefin hydrocarbon under polymerization conditions including a temperature in the range of 0 to 150 C'. with a polymerization catalyst consisting essentially of nely .dividednickel oxide in minor proportion dispersedl on silica gel containing a promoting amount of alumina in the rangeof 0.1 to,v 10

16 4; A proccssfor pol'ymerizing4 ethylenetoform higher; molecular'weight. aliphatic olefin hydrocarbons which comprises contacting ethylene under polymerization conditions including a temperature in the range of 0 to. 150 C. with a polymerization catalystA consisting essentially of a minor proportion of,v nickel oxide dispersed on ay major proportion of silica gel containing an amount of alumina as a promoter in the range of 1 to 10 weight' per cent based on the Weight of the silicagel, the nickel in saidnickel oxide rangingk from 0.1 to 5. Weight per cent of the silica gel, said catalyst havingr been activated by heating ,in an oxidizing atmosphere at a temperature inthe range ofl 400 to 700 C. for a time in the range of v0.5 to 12 hours.

GRANT C. BAILEY; JAMES A. REID'.

REFERENCES CITED The4 following references are of record in the le of this patent:

UNITED STATESPA'I'ENTS Number Name Date 1,256,032 Mittaschr Feb. 12, 1918 1,925,820 Reyerson Sept. 5, 1933 1,933,091 Bertsch Oct. 31, 1933 2,181,640 Deanesley et al Nov. 28, 1939 2,332,276 StahlyV Oct. 19, 1943 2,349,904 Hachmuth May 30, 1944 2,355,388 Michael et al. Aug. 8, 1944 2,377,411 Frey June 5, 1945 2,380,358 Anderson et al July 10, 1945 2,381,198 Bailey et al. Aug. 7, 1945 2,385,609 Clark'et al Sept. 25,1945 

1. A PROCESS FOR POLYMERIZING A NORMALLY GASEOUS OLEFIN HYDROCARBON TO FORM HIGHER MOLECULAR WEIGHT OLEFIN HYDROCARBONS WHICH COMPRISES CONTACTING SUCH AN OLEFIN HYDROCARBON UNDER POLYMERIZATION CONDITIONS INCLUDING A TEMPERATURE IN THE RANGE OF 0* TO 150* C. WITH A POLYMERIZATION CATALYST CONSISTING ESSENTIALLY OF A MINOR PROPORTION OF NICKEL OXIDE DISPERSED ON A MAJOR PROPORTION OF SILICA GEL CONTAINING AN AMOUNT OF ALUMINA AS A PROMOTER IN THE RANGE OF
 1. TO 10 WEIGHT PER CENT BASED ON THE WEIGHT 